CN107011935A - 生物来源的烃的生产方法 - Google Patents
生物来源的烃的生产方法 Download PDFInfo
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- CN107011935A CN107011935A CN201610825834.5A CN201610825834A CN107011935A CN 107011935 A CN107011935 A CN 107011935A CN 201610825834 A CN201610825834 A CN 201610825834A CN 107011935 A CN107011935 A CN 107011935A
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- isomerization
- catalyst
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- seethed
- excitement
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
- C10G3/46—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof in combination with chromium, molybdenum, tungsten metals or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/47—Catalytic treatment characterised by the catalyst used containing platinum group metals or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
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Abstract
本发明涉及烃,特别是涉及适于用作航空燃料或喷气燃料以及用作航空燃料用调合料的烃组分的生产。本发明方法包括下述阶段,其中在第一阶段中,使生物来源的油进料和氢气在加氢脱氧催化剂存在下经历足以进行加氢脱氧的条件,以得到正构链烷烃;在第二阶段中,使该正构链烷烃和氢气在异构化催化剂存在下经历足以进行异构化的条件以得到异链烷烃并且分离馏分;并且将从第二阶段获得的在大气压力下在200℃或更高温度下沸腾的馏分再循环到进行再异构化,其中在异构化催化剂存在下进行异构化。
Description
技术领域
本发明涉及烃,特别是涉及适于用作航空燃料或喷气燃料以及用作航空燃料用调合料的烃组分的生产。本发明还涉及由生物来源的可再生原料生产烃的方法。特别地,本发明提供了基于生物原料生产高质量航空燃料或航空燃料用组分或调合料的可替代方法。
背景技术
航空燃料或喷气燃料通常由粗矿物油生产,该粗矿物油通常通过蒸馏被分离得到在航空燃料馏程内沸腾的直馏煤油馏分,并且在需要时在之后进行本领域中公知的任选的转换过程如裂化等。还可以例如通过加氢处理或通过直馏煤油的碱洗来生产满足航空燃料要求的衍生自矿物油的煤油。
费-托法被越来越多地用于生产航空燃料,在其中一氧化碳和氢气在含铁、钴、镍或钌的催化剂上反应,生成直链和支链烃以及更少量的含氧化合物的混合物。用作原料的合成气可衍生自煤、天然气、生物质或重油物流。主要包含线性链烷烃的所得混合物被分馏,并且在航空燃料馏程内沸腾的馏分被分离并用作航空涡轮燃料中的组分,如 WO2007/110448中所述。
US 2006/0111599描述了一种在其中将改进的低温费-托(LTFT)进料分馏并任选地掺混以获得低硫航空涡轮燃料的方法。获得的产品具有约270℃的终沸点,通常包含异链烷烃和正构链烷烃的掺混物。
WO 2007/027955提供了一种制备适于用作喷气燃料的烃产品的方法。在该方法中,使含C10-C20脂肪酸的进料(来源于任何甘油三酯源)进行热脱羧作用,接着将所得产品与含烯烃的材料混合并且进行烯烃复分解,然后进行脱氢作用(如果复分解产品是饱和的话),随后进行任选的加氢作用。
WO 2007/027669教导了一种制备适于用作喷气燃料的烃产品的方法。在所述方法中,使含C10-C20脂肪酸的进料(来源于任何甘油三酯源)进行Kolbe电解而获得产物,将该产物与含烯烃的材料混合并且进行烯烃复分解,然后进行脱氢作用(如果复分解产品是饱和的话),随后进行任选的异构化。
通常航空涡轮燃料包含使用不同方法获得的馏分和组分的掺混物。
专利FI 100248描述了一种用于生产中间馏分的两步法,其中将植物油中所含的脂肪酸和脂肪酸的甘油三酯氢化而得到正构链烷烃,随后将正构链烷烃异构化生成异链烷烃。获得的烃产品具有低(cold) 温性能,不适合用作航空燃料。
航空燃料的典型特征如下所述。航空燃料是一种其大于90%的体积在130到300℃范围内沸腾(ASTM D86)、密度在15℃温度时为775 到840kg/m3范围内,优选780到830kg/m3范围内(ASTM D4052)、初沸点在130-160℃范围内、终沸点在220-300℃范围内(ASTM D86)、-20℃温度下运动粘度在1.2-8.0mm2/s范围内(ASTM D445)、凝固点低于-40℃,优选低于-47℃(ASTM D2386)、并且闪点至少38℃(IP 170)的产品。
在多个标准中定义了对于航空涡轮燃料质量和性能的最低要求。在标准DEF STAN91-91(英国国防部标准DEF STAN 91-91/2008年4 月8日第6期,关于涡轮燃料、航空煤油型、喷气A-1、NATO代号 F-35、联合服务名称AVTUR或检验时的当前版本)或在“检查单”(对联合操作系统的航空燃料质量要求,AFQRJOS)中的喷气A-1要求是基于ASTM D1655、DEFSTAN 91-91和IATA、用于航空涡轮燃料规范的指导材料、某些机场操作要求的最严格要求。“半合成”航空燃料以DEF STAN 91-91在1999年被批准,并且全合成喷气燃料在2008 年被批准。满足AFORJOS技术条件要求的航空燃料被称作“按照检查单的喷气A-1”或“检查单喷气A-1”燃料。
关于异链烷烃航空涡轮燃料的使用出现了一些问题,涉及到润滑性、热稳定性、氧化稳定性、储存稳定性、水分离特性、抗凝固性能和导电性。因此常常需要合适的添加剂来解决所述问题。允许在航空燃料中同时使用至多5种不同的合格添加剂,在航空燃料中使用通常 1到3种不同的添加剂,该添加剂选自罗列于DEF STAN 91-91/6中被批准的添加剂。
防静电添加剂(SDA)总是需要的,以用于调节和保持操作条件下的电导率高于50pS/m。它在使用现代快速加燃料设备时在加燃料条件下是特别重要的。如果燃料的电导率不足,所述设备可导致静电的形成,这可引起火花甚至严重的加燃料火灾。
抗氧化剂通常被使用以用于改善燃料的稳定性,并且它们减少或防止燃料储存期间沉淀物的形成。
润滑改进添加剂(LIA)用于改善润滑性,并且它们同时在航空燃料中起到腐蚀抑制剂的作用,尤其是在军事用途中,并且当产品含有大于95%的加氢处理的产品时。
金属钝化剂(MDA)防止金属与燃料反应,这显著降低热稳定性。
燃料体系结冰抑制剂(FSII)主要用在军事实践中。
化石航空燃料的可获得性在未来将会减少,因此明显需要提供用于生产航空涡轮燃料的可替代来源和方法。此外可以预期,空中交通在未来将会增加,导致对于航空燃料的需求增加。对于减少对环境和健康的危害和问题的要求越来越严格,并且总的目标是提供对环境较少危害的航空燃料。目标还在于将排放削减到明显更低的水平,并且特别是显著降低二氧化碳的排放。还可以看到越来越令人感兴趣的是,开发基于可再生材料的新燃料,而不是使用衍生自原油等化石材料的产品。
基于以上的情况,可以看到对于用于生产适于作为高质量航空燃料或作为所述燃料用调合料的烃组分的新的且改进的方法存在明显的需求,该方法能够避免或至少显著降低与目前航空燃料及其生产有关的问题。另外需要在所述生产方法中使用基于可再生资源的原料。
发明目的
本发明的目的是生产烃的方法。
本发明的另一目的是生产适于作为航空燃料或航空燃料用调合料的烃组分的方法。
本发明的又一目的是由生物且可再生原料生产航空燃料或航空燃料用调合料的方法。
本发明的再一目的是由生物且可再生原料生产符合喷气A-1要求的航空燃料用调合料或组分的方法。
本发明的特性特征在权利要求中提供。
定义
在本文中航空燃料应理解为是指适于航空目的的航空涡轮燃料或喷气燃料。
生物喷气燃料是指来源于生物原料的航空燃料。
在本文中加氢处理应理解为通过任何分子氢方式对有机材料进行催化处理。
在本文中加氢处理应理解为一种催化过程,该过程从有机氧化合物中以水的形式去除氧(加氢脱氧,HDO),从有机硫化合物中以硫化二氢(H2S)的形式去除硫(加氢脱硫,HDS),从有机氮化合物中以氨 (NH3)的形式去除氮(加氢脱氮,HDN)以及去除卤素,例如从有机氯化合物中以氢氯酸(HCl)的形式去除氯(加氢脱氯,HDCl),通常在催化剂的影响下进行。
在本文中脱氧应理解为从有机分子如脂肪酸衍生物、醇、酮、醛或酯中通过先前所述的任何措施去除氧。
在本文中甘油三酯或其它脂肪酸衍生物或脂肪酸的加氢脱氧 (HDO)应理解为在催化剂的影响下借助于分子氢以水的形式去除羧基氧。
在本文中甘油三酯或其它脂肪酸衍生物或脂肪酸的脱羧和/或脱羰应理解为在有或没有分子氢的影响下以CO2形式(脱羧)或以CO形式(脱羰)去除羧基氧。
在本文中加氢裂化应理解为在高压下使用分子氢催化分解有机烃材料。
在本文中加氢是指在催化剂的影响下借助于分子氢的碳-碳双键的饱和。
在本文中正构链烷烃(n-paraffins)是指不含侧链的正链烷烃或线性链烷烃。
在本文中异链烷烃(isoparaffins)是指具有一个或多个C1-C9,通常是C1-C2烷基侧链的链烷烃,通常是单-、二-、三-或四甲基链烷烃。
第一方法步骤的进料(总进料)被理解为包含新鲜进料和任选的至少一种稀释剂。
典型的气体(gas)沸程是从-162到40℃,典型地包含C1-C5烃。
典型的汽油沸程是从40到210℃,典型地包含C5-C10烃。
典型地,航空燃料包含C8-C16烃,并且典型地,初沸点在130到 160℃范围内,终沸点在220到300℃范围内。
典型的柴油燃料沸程是从160到360℃,典型地包含C10-C28烃。
沸腾温度指在标准大气压下的温度,除非另有指明。
本发明涉及生产烃和烃组分的方法。所得烃组分可用作高质量航空燃料和高质量航空燃料用组分(components)或调合料(blending stocks)。此外还获得可用作柴油燃料的烃组分以及适于作为气体和汽油的组分。
该方法包括以下阶段,其中得自可再生来源的进料进行加氢脱氧和异构化,然后分离在气体馏程中、在汽油馏程中、在航空燃料馏程中沸腾的馏分并且任选地分离在柴油燃料馏程中沸腾的馏分,并且然后使在大气压下在200℃或更高的温度下(特别是从≥200℃到650℃) 沸腾的馏分(来自于异构化的重再循环物流)并且任选地使在柴油燃料馏程中沸腾的馏分进行第二异构化。使用任何合适的分离技术将产品分离成各组分。
获得包含异链烷烃的烃组分,在航空燃料馏程中沸腾的组分特别适于作为异链烷烃航空燃料或作为航空燃料用调合料。可获得具有优异的低温性能,特别是具有非常低的凝固点,甚至满足喷气A-1级要求的航空燃料和航空燃料用调合料。
根据本发明的方法包括加氢脱氧阶段,接着是异构化阶段,然后从异构化的产品中分离较轻的馏分,并且将在200℃或更高的温度下沸腾的馏分(重再循环物流)再异构化。
特别地,该方法包括以下阶段,其中在第一阶段(加氢脱氧),使生物来源的油进料(feed)和氢气在加氢脱氧催化剂存在下经历足以进行加氢脱氧的条件,以得到正构链烷烃;
在第二阶段(异构化),使该正构链烷烃和氢气在异构化催化剂存在下经历足以进行异构化的条件,以得到异链烷烃;以及
分离在气体馏程中、在汽油馏程中、在航空燃料馏程中沸腾的馏分并且任选地分离在柴油燃料馏程中沸腾的馏分,再异构化(第二异构化)在200℃或更高温度下沸腾的馏分(重再循环物流)以及任选地在柴油燃料馏程中沸腾的馏分,这在异构化催化剂的存在下进行;并且
然后分离所获得的异链烷烃型烃组分。
再异构化可以以三种可选方式进行:
1)该重再循环物流(heavy recycle stream)和任选地在柴油燃料馏程中沸腾的馏分或者其一部分被再循环并且与送入第二阶段(异构化) 的进料混合并且进行异构化;或者
2)该重再循环物流和任选地在柴油燃料馏程中沸腾的馏分或者其一部分被再循环并且被送到包括至少两个区段(section)的第二阶段(异构化)的第一区段并且进行异构化,从第一阶段(加氢脱氧)获得的正构链烷烃被送到该异构化阶段的第二区段并且进行异构化;或者
3)该重再循环物流和任选地在柴油燃料馏程中沸腾的馏分或者其一部分被再循环并且被送到第三阶段(异构化)并且进行异构化。
具体实施方式
在图1中,在第一反应阶段(加氢脱氧),以物流1表示的经预处理的进料与以物流2表示的再循环气体混合,该再循环气体是再循环的气体和补充氢气8的混合物。合并的物流3被送到包含加氢脱氧催化剂的反应区段A的催化剂床。反应区段A可包括一个或多个催化剂床。来自于反应区段A的经加氢脱氧的流出物4进入分离器B(例如汽提器(stripper)),并且包含氢气、轻气体、CO2和水的蒸气物流5被送到气体纯化区段F,用于气体纯化和再循环。来自于分离器B的蒸气物流6被送到气体纯化区段F,用于气体纯化和再循环,并且液体物流7与氢气物流8合并。在第二反应阶段(异构化),合并的物流9进入包含异构化催化剂的反应区段C。反应区段C可包括一个或多个催化剂床。来自于反应区段C的经异构化的液体流出物10被送到分馏器D,在其中通过蒸馏分离在气体馏程12、汽油馏程13、航空燃料馏程14沸腾的馏分,以及任选地,在柴油燃料馏程15沸腾的馏分或者其一部分。任选地与馏分15或者其一部分合并的重再循环物流,即馏分16以物流17再循环,物流17与物流9合并。包含氢气、轻气体、 CO2和水的蒸气物流11被送到气体纯化区段F,用于气体纯化和再循环。任选地,取出物流16的一部分作为物流18用作柴油燃料组分。
在图2中,在第一反应阶段(加氢脱氧),以物流1表示的经预处理的进料与以物流2表示的再循环气体混合,该再循环气体是再循环的气体和补充氢气8的混合物。合并的物流3被送到包含加氢脱氧催化剂的反应区段A的催化剂床。反应区段A可包括一个或多个催化剂床。来自于反应区段A的经加氢脱氧的流出物4进入分离器B(例如汽提器),并且包含氢气、轻气体、CO2和水的蒸气物流5被送到气体纯化区段F,用于气体纯化和再循环。来自于分离器B的蒸气物流6被送到气体纯化区段F,用于气体纯化和再循环,并且液体物流7与氢气物流8合并。在第二反应阶段(异构化),合并的物流9进入包括至少两个子区段C1和C2的反应区段C的第二子区段C2的催化剂床,其包含异构化催化剂。反应区段C在每个子区段C1和C2中可包含一个或多个催化剂床。来自于反应区段C的经异构化的液体流出物10被送到分馏器D,在其中通过蒸馏分离在气体馏程12、汽油馏程13、航空燃料馏程14沸腾的馏分,以及任选地,在柴油燃料馏程15沸腾的馏分或者其一部分。任选地与馏分15或者其一部分合并的重再循环物流,即馏分16以物流17再循环,物流17与氢气物流8合并,并且合并的物流19被送到反应区段C的第一子区段C1的催化剂床。包含氢气、轻气体、CO2和水的蒸气物流11被送到气体纯化区段F,用于气体纯化和再循环。任选地,取出物流16的一部分作为物流18用作柴油燃料组分。
在图3中,在第一反应阶段(加氢脱氧),以物流1表示的经预处理的进料与以物流2表示的再循环气体混合,该再循环气体是再循环的气体和补充氢气8的混合物。合并的物流3被送到包含加氢脱氧催化剂的反应区段A的催化剂床。反应区段A可包括一个或多个催化剂床。来自于反应区段A的经加氢脱氧的流出物4进入分离器B(例如汽提器(stripper)),并且包含氢气、轻气体、CO2和水的蒸气物流5被送到气体纯化区段F,用于气体纯化和再循环。来自于分离器B的蒸气物流6被送到气体纯化区段F,用于气体纯化和再循环,并且液体物流7与氢气物流8合并。在第二反应阶段(异构化),合并的物流9进入包含异构化催化剂的反应区段C。反应区段C可包括一个或多个催化剂床。来自于反应区段C的经异构化的液体流出物10被送到分馏器D,在其中通过蒸馏分离在气体馏程12、汽油馏程13、航空燃料馏程14沸腾的馏分,以及任选地,在柴油燃料馏程15沸腾的馏分或者其一部分。任选地与馏分15或者其一部分合并的重再循环物流,即馏分16以物流17再循环,物流17与氢气物流8合并。在第三反应阶段 (异构化),合并的物流19被送到包含异构化催化剂的反应区段E。反应区段E可包括一个或多个催化剂床。经异构化的液体流出物20与物流10合并,并且被送到分馏器D,并且蒸气物流21被送到气体纯化区段F,用于气体净化和再循环。任选地,取出物流16的一部分作为物流18用作柴油燃料组分。
每个反应区段可包括一个或多个催化剂床。
任选地,来自于反应区段C的液体流出物10的一部分可被再循环并且与物流9合并(在图中未表示)。
任选地,在柴油燃料馏程中的馏分或者其一部分可以与该重再循环物流合并,并且进行再异构化,这取决于该方法的优化和操作。
令人惊奇地发现,利用本发明的方法能够获得适于作为高质量航空燃料或高质量航空燃料用组分或调合料的烃,特别是异链烷烃型烃组分,该方法包括以下阶段,其中在第一阶段,使生物来源的油进料和氢气在加氢脱氧催化剂存在下经历足以进行加氢脱氧的条件,以得到正构链烷烃;
在第二阶段,使该正构链烷烃和氢气在异构化催化剂存在下经历足以进行异构化的条件,以得到异链烷烃;以及
将任选地与在柴油燃料馏程中沸腾的馏分或者其一部分合并的从第二阶段获得的在大气压力下在200℃或更高温度下(特别是从≥200℃到650℃)沸腾的馏分(重再循环物流)再循环到进行再异构化 (reisomerisation),其中在异构化催化剂存在下进行异构化。取决于蒸馏设备和柴油燃料或航空燃料组分所希望的收率,该重再循环物流可以是包含在250℃或更高温度下沸腾的馏分或者在290℃或更高温度下沸腾的馏分,在两种情况下的沸程的上限是650℃,如果需要的话。
该再异构化可以以三种可选方式来进行:
1)该重再循环物流(在200℃或更高温度下沸腾的馏分)和任选地在柴油燃料馏程中沸腾的馏分或者其一部分被再循环并且与供给第二阶段(异构化)的进料混合并且进行再异构化;或者
2)该重再循环物流(在200℃或更高温度下沸腾的馏分)和任选地在柴油燃料馏程中沸腾的馏分或者其一部分被再循环并且被送到包括至少两个区段的第二阶段(异构化)的第一区段并且进行异构化,从第一阶段(加氢脱氧)获得的正构链烷烃被送到该异构化阶段的第二区段并且进行异构化;或者
3)该重再循环物流(在200℃或更高温度下沸腾的馏分)和任选地在柴油燃料馏程中沸腾的馏分或者其一部分被再循环并且在第三阶段(异构化)中进行异构化。
本发明优选的实施方案描述如下。本发明的方法包括至少两个阶段,每个阶段具有至少一个反应区(zone),所述方法包括如下步骤:
a)将生物来源的油进料(feed)与包含氢气的气体物流合并以形成原料(feedstock);
b)将该原料送到第一阶段的反应区,其保持在足以进行加氢脱氧的条件下,并且将该原料与加氢脱氧催化剂接触;
c)将来自步骤(b)的流出物送到分离器,其在此被分离成塔顶馏分和塔底馏分;
d)将来自步骤(c)的塔底馏分与含氢气的气体物流混合;
e)将来自步骤(d)的合并的物流送到第二阶段的反应区段,其保持在足以进行异构化的条件下,并且将该物流与异构化催化剂接触;
f)将来自步骤(e)的流出物送至进行分馏,从而产生异构化的产物物流,移除在气体馏程中沸腾的物流,在汽油馏程中沸腾的物流,在航空燃料馏程中沸腾的物流,以及任选地,在柴油燃料馏程中沸腾的物流或者其一部分;
g)将在200℃或更高温度下沸腾的馏分(重再循环物流)和任选的来自步骤(f)的在柴油燃料馏程中沸腾的馏分或者其一部分再循环至进行再异构化。
该再异构化可以以如上所述的可选方式来进行。
原料(feedstock)
在本发明方法中用作新鲜油进料的生物油和/或脂肪来源于生物且可再生资源如植物和/或动物和/或鱼类和/或昆虫,以及来源于利用微生物如藻类、细菌、酵母和霉菌的过程,并且合适的还有衍生自所述脂肪和油及其混合物的化合物。产生生物油或脂肪的物种可以是天然的或者基因工程的。生物油和脂肪可以是直馏油和脂肪或再循环的油和脂肪。
典型的植物或动物油/脂肪的基本结构单元为甘油三酯,即甘油与三个脂肪酸分子的三酯,具有在下式I中示出的结构:
式I:甘油三酯的结构
在式I中,R1,R2和R3为烷基链。在天然甘油三酯中存在的脂肪酸几乎是单独的偶碳数的脂肪酸。因此,R1,R2和R3典型地是 C5-C23烷基,主要是C11-C19烷基,最典型地是C15或C17烷基。R1, R2和R3可包含碳-碳双键。这些烷基链可以是饱和的、不饱和的或聚不饱和的。
含脂肪酸和/或脂肪酸酯和/或脂肪酸衍生物的合适的生物油是木基和其它植物基和蔬菜基脂肪和油,例如油菜籽油、菜油、芥花籽油、妥尔油、麻风树籽油、向日葵油、大豆油、大麻籽油、橄榄油、亚麻籽油、芥子油、棕榈油、花生油、蓖麻油、椰子油,以及在通过基因操作繁殖的植物中所含的脂肪,动物基脂肪如猪油、牛油、鲸油,以及在牛奶中所含的脂肪,以及食品工业的再循环脂肪以及以上物质的混合物,以及源于利用微生物如藻类、细菌、酵母和霉菌的过程的脂肪和油。
适于作为新鲜进料的生物油和脂肪包含C12-C24脂肪酸,其衍生物如脂肪酸的酐或酯以及脂肪酸的甘油三酯和甘油二酯或者其组合。脂肪酸或脂肪酸衍生物如酯可以通过生物油的水解或者通过它们的分馏或者甘油三酯的酯交换反应或者利用微生物的微生物学过程来生产。
为了避免催化剂失活和不希望的副反应,有利的是进料符合以下要求:碱金属和碱土金属的量以元素碱金属和碱土金属计算在进料中为低于10优选低于5mg/kg。其它金属的量以元素金属计算在进料中为低于10优选低于5mg/kg。磷的量以元素磷计算为低于30优选低于 15mg/kg。
在许多情况下,油进料如粗植物油或动物脂肪因为杂质含量高而不适合原样用于处理,因此该进料优选在被引入到该方法的加氢脱氧步骤之前使用一种或多种传统纯化操作程序进行预处理。一些传统纯化/预处理操作程序的例子提供如下。
植物油/脂肪和动物油/脂肪的脱胶是指去除磷化合物如磷脂。经溶剂萃取的植物油常常含有显著量的胶质,其主要是磷脂类(磷脂)。铁以及其它金属也可以金属-磷脂类配合物的形式存在。
通常如下进行脱胶:在升高的温度和压力下使用酸、碱和软水洗涤进料并且分离形成的胶质,另外主要量的金属成分也被除去。
任选地以另一种传统方式脱胶或精制的进料可以利用天然或酸活化的漂白粘土进行漂白。漂白操作去除了其它预处理步骤留下的各种杂质痕迹,例如叶绿素、类胡萝卜素、磷脂、金属、皂和氧化产物。通常,漂白的目的在于减少有色颜料并降低油的氧化趋势。
任选地,在加氢脱氧之前,为了防止不饱和甘油三酯的双键聚合,可以在降低的反应温度和合适的催化剂下通过预氢化双键来分解进料中的甘油三酯结构。
以下将更加详细地描述加氢脱氧阶段和异构化阶段。
加氢脱氧
在加氢脱氧阶段,将进料中所含的脂肪酸、甘油三酯和其它脂肪酸衍生物脱氧、脱氮和脱硫。
在加氢脱氧阶段,反应条件包括压力为10至150巴,优选30至 70巴;温度为200至400℃,优选250至350℃,最优选280至340℃;进料速率(LHSV)为0.1-10hr-1(v/v)。
在加氢脱氧阶段,可以使用包含来自于元素周期系第VIII族和/ 或VIB族的金属的已知加氢催化剂。优选地,加氢催化剂为负载的 Pd、Pt、Ni、NiMo或CoMo催化剂,载体为氧化铝和/或二氧化硅,如FI 100248中所述。典型地,使用NiMo/Al2O3和CoMo/Al2O3催化剂。
与未受控的裂化相反,甘油三酯的加氢脱氧有利于甘油三酯分子的受控分解。在受控加氢处理期间双键也被氢化。从加氢脱氧的产物中除去所形成的轻质烃和气体,主要是丙烷,水,CO2,CO,H2S和 NH3。
任选地,该进料可包括新鲜进料和选自烃和该方法的再循环产物的至少一种稀释剂。
有机或无机硫化合物可以任选地随同氢气一起或随同进料一起供应,以促进在脱碳反应(decarb-reactions)时进行脱氧,如果需要的话。
加氢脱氧阶段之后是异构化阶段。
在根据本发明的方法中,进入异构化反应器的进料是正构链烷烃的混合物,且其组成可以从该进料的各生物油的脂肪酸分布来预测。在该方法的加氢处理步骤的过程中,甘油三酯油和其它脂肪酸衍生物和脂肪酸理论上几乎均转化为正构链烷烃。另外,丙烷从甘油三酯的甘油部分、水和COX从羧基氧、H2S从有机硫化合物并且NH3从有机氮化合物形成。对于该方法来说有利的是,在烃与异构化催化剂接触前去除这些气相杂质。
使来自加氢脱氧阶段的反应产物进行分离,并且包含正构链烷烃的流出物被送到第二阶段,即进行异构化。
异构化
在异构化阶段中,反应条件包括压力为10至150巴,优选30至 100巴;温度为200至500℃,优选280至400℃;进料速率(LHSV) 为0.1-10hr-1(v/v)。
在异构化阶段中,可以使用本领域中已知的异构化催化剂。合适的异构化催化剂包含分子筛和/或选自元素周期表第VIII族的金属和/ 或载体。优选地,该异构化催化剂包括SAPO-11或SAPO-41或ZSM-22 或ZSM-23或镁碱沸石和Pt、Pd或Ni和Al2O3或SiO2。典型的异构化催化剂例如是Pt/SAPO-11/Al2O3、Pt/ZSM-22/Al2O3、 Pt/ZSM-23/Al2O3和Pt/SAPO-11/SiO2。这些催化剂中的大部分要求存在氢以减少催化剂的失活。
图2和3描述了本发明的优选实施方案。
在图2所述的实施方案中,异构化反应区段C包括至少两个子区段C1和C2,在每个区段中可以使用相同或不同的催化剂和相同或不同的温度。
在根据图3描述的实施方案的其中再异构化作为第三阶段实施 (异构化)的本发明可选方案中,在每个异构化阶段中可以使用相同或不同的催化剂以及相同或不同的反应条件。例如,在第一异构化阶段,可以选择不利于裂化的催化剂和/或反应条件,在第二异构化阶段,可以选择促进裂化的催化剂和/或反应条件,从而使得组分的收率增加或者使产品具有所希望的低温性能。
该方法得到的烃组分适于作为生物喷气燃料和航空燃料用调合料,还获得适于作为柴油燃料、汽油和气体的组分。
可获得满足喷气A-1要求的航空燃料,其包含使用本发明方法生产的组分,并与传统航空燃料掺混。
令人惊奇地发现,可以从生物且可再生材料以及从其任何混合物以非常好的收率获得特别适于作为高质量航空燃料和航空燃料用组分的异链烷烃型烃组分。航空燃料收率是非常高的。在加氢脱氧阶段形成的重组分(重再循环物流)以一种有效且经济的方式被利用,并且它们被转化为在低温下也具有特别好的性能的更有价值的组分,因而使其特别适用于航空燃料。与进行一次异构化的方法相比,在本发明方法中C18和C20组分的转化是显著更高的。典型地,使重组分进行异构化以及一定程度上的裂化。包括加氢脱氧、异构化和再异构化的该方法使得包含高度支化异链烷烃的产物的凝固点显著降低。在本发明的方法中,特别地,在更高温度下沸腾且降低了凝固点和倾点的组分被进一步处理成具有更有利性能的组分。
该产物不含烯烃,不含芳族化合物或环烷烃,这显著降低了发动机的结垢。该产物基于可再生材料并且不含硫化合物。
使用以下实施例更进一步地阐明本发明,但其并不对本发明范围构成限制。
实施例
实施例1
在第一阶段中,在固定床管式反应器中进行棕榈油的加氢脱氧。该反应在NiMo催化剂存在下,在47巴压力下进行,WHSV为0.5l/h,反应温度为330℃。氢油比约为1000标准升H2/升油进料。产物油(正构链烷烃)不含氧化合物。
在第二阶段中,使以上获得的产物油在Pt-SAPO-催化剂存在下,在固定床管式反应器中进行异构化,压力为37巴,WHSV为1.3l/h,反应温度为313℃。氢油比约为300标准升H2/升油进料。
将从异构化阶段获得的产物分馏,并且重再循环物流(在290℃和更高温度下沸腾的馏分)被送入第三阶段(第二异构化),在此在固定床管式反应器中在Pt-SAPO-催化剂存在下进行再异构化,压力为40巴, WHSV为1.5l/h,氢油比为300标准升H2/升油进料。使用315℃的反应温度,在该情况下产物被分馏得到柴油燃料EN590,322℃时为航空燃料,喷气燃料1,340℃时为喷气燃料2。
从第一异构化获得的产物、供给第二异构化的进料(重再循环物流)、最终产物柴油燃料和航空燃料的特性列于下表1中。
表1产物的特性
Claims (8)
1.用于生产烃的方法,所述方法包括下述阶段,其中在第一阶段中,使生物来源的油进料和氢气在加氢脱氧催化剂存在下经历足以进行加氢脱氧的条件,以得到正构链烷烃;
在第二阶段中,使该正构链烷烃和氢气在异构化催化剂存在下经历足以进行异构化的条件以得到异链烷烃并且分离馏分;并且
将从第二阶段获得的在大气压力下在200℃或更高温度下沸腾的馏分再循环到进行再异构化,其中在异构化催化剂存在下进行异构化。
2.根据权利要求1所述的方法,其特征在于在200℃或更高温度下沸腾的馏分被再循环并且与供给第二阶段的进料合并,并且进行再异构化。
3.根据权利要求1所述的方法,其特征在于在200℃或更高温度下沸腾的馏分被再循环并且被送到包括至少两个区段的第二阶段的第一区段并且进行异构化,从第一阶段获得的正构链烷烃被送到第二阶段的第二区段并且进行异构化。
4.根据权利要求1所述的方法,其特征在于在200℃或更高温度下沸腾的馏分被再循环并且在异构化催化剂存在下在第三阶段中进行再异构化。
5.根据权利要求1-4中任一项所述的方法,其特征在于在200℃或更高温度下沸腾的馏分与在柴油燃料馏程中沸腾的馏分或者其一部分合并。
6.根据权利要求1-5中任一项所述的方法,其特征在于在第一阶段中,加氢脱氧在加氢催化剂存在下在10至150巴的压力和200至400℃的温度下进行,所述加氢催化剂包含选自元素周期系第VIII和/或VIB族的金属。
7.根据权利要求1-6中任一项所述的方法,其特征在于在第二阶段中,异构化在异构化催化剂存在下在10至150巴的压力和200至500℃的温度下进行,所述异构化催化剂包含分子筛和/或选自元素周期表第VIII族的金属。
8.根据权利要求4-7中任一项所述的方法,其特征在于在第三阶段中,异构化在异构化催化剂存在下在10至150巴的压力和200至500℃的温度下进行,所述异构化催化剂包含分子筛和/或选自元素周期表第VIII族的金属。
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CN113166664A (zh) * | 2018-12-14 | 2021-07-23 | 耐思特公司 | 柴油燃料组合物 |
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KR20110044950A (ko) | 2011-05-03 |
EA021734B1 (ru) | 2015-08-31 |
UA102696C2 (ru) | 2013-08-12 |
EP2141217B1 (en) | 2015-03-25 |
WO2010000934A1 (en) | 2010-01-07 |
BRPI0913848A2 (pt) | 2016-05-17 |
NZ590189A (en) | 2012-06-29 |
BRPI0913848B1 (pt) | 2023-01-10 |
EA201170120A1 (ru) | 2011-08-30 |
MX343002B (es) | 2016-10-21 |
PT2141217E (pt) | 2015-07-30 |
ES2540063T3 (es) | 2015-07-08 |
ZA201009300B (en) | 2011-09-28 |
JP2011526640A (ja) | 2011-10-13 |
AP2010005516A0 (en) | 2010-12-31 |
CN102124080A (zh) | 2011-07-13 |
MY155339A (en) | 2015-10-15 |
PL2141217T3 (pl) | 2015-08-31 |
AP3333A (en) | 2015-07-31 |
EP2141217A1 (en) | 2010-01-06 |
AU2009265573A1 (en) | 2010-01-07 |
AU2009265573B2 (en) | 2016-01-07 |
CA2729651A1 (en) | 2010-01-07 |
JP5506791B2 (ja) | 2014-05-28 |
DK2141217T3 (en) | 2015-06-15 |
MX2011000015A (es) | 2011-08-03 |
KR101335925B1 (ko) | 2013-12-03 |
CA2729651C (en) | 2015-04-14 |
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